CN1662632A - Process to prepare medicinal and technical white oils - Google Patents
Process to prepare medicinal and technical white oils Download PDFInfo
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- CN1662632A CN1662632A CN038146940A CN03814694A CN1662632A CN 1662632 A CN1662632 A CN 1662632A CN 038146940 A CN038146940 A CN 038146940A CN 03814694 A CN03814694 A CN 03814694A CN 1662632 A CN1662632 A CN 1662632A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/14—White oil, eating oil
Abstract
Process for the preparation of medicinal white oil or a technical white oil from a Fischer-Tropsch derived paraffinic distillate bottom product, wherein said bottom product is contacted with a heterogeneous absorbent.
Description
The present invention relates to a kind of preparation from the medicinal white oils of Fischer-Tropsch process and the method for industrial white oil.Described medicinal white oils preferably the kinematic viscosity in the time of 100 ℃ greater than 8.5cSt.
The applicant has developed a kind of novel method, and this method can be prepared various base oil levels simultaneously by the fischer-tropsch synthesis product than heavy, comprises high viscosity grade.Such fischer-tropsch synthesis product for example can obtain with method described in the WO-A-9934917.
This novel method comprises described raw material hydrotreatment, and preferably then carries out the depression of pour point step.For example at different material this method has been described among the embodiment 3 of EP-A-776959.Kinematic viscosity when the kinematic viscosity the when cut that obtains with the raw material than heavy can be separated into 100 ℃ by underpressure distillation subsequently is at least the heavy base oil level of 8.5cSt and 100 ℃ is one or more base oil levels of 2-7cSt.Its performance equals or can obtain with high yield as the base product product near the heavy base oil of industrial white oil.
When producing product with fischer-tropsch synthesis product, be not easy to occur color problem, because the raw material of Fischer-Tropsch process is very pure, and in general, form the aromatic substance that has color hardly.But the applicant has been found that: in our lab setup, this heavy tower bottom distillate is light yellow at least.Cause this base oil directly not use because of this color as industrial white oil.
The feature of industrial white oil and medicinal white oils is that they do not have color.The Saybolt color of industrial white oil (Saybolt colour) (ASTM D-156) is greater than+20.The Saybolt color of medicinal white oils is greater than+25, more particularly equal+30.The specification of other medicinal white oils and industrial white oil is respectively according to having low UV adsorptive capacity as FDA 178.3620 (b) with FDA 178.3620 (`c) in different UV spectral ranges.Be used in medicinal white oils in the field of food also need be in the time of 100 ℃ greater than the kinematic viscosity of 8.5cSt and 5wt% boiling point greater than 391 ℃.
The applicant finds now: the industrial white oil that do not reach required specification or medicinal white oils are contacted with heterogeneous sorbent material can not obtain medicinal white oils or industrial white oil.Therefore, the present invention relates to a kind of being used for wherein makes described bottom product contact with heterogeneous sorbent material from the paraffinic hydrocarbons base product product preparation medicinal white oils of Fischer-Tropsch process or the method for industrial white oil.
The example of suitable heterogeneous sorbent material is a gac; Zeolite is as natural faujasite or synthetic materials such as ferrierite, ZSM-5, faujusite, mordenite; Metal oxide such as SiO 2 powder, silica dioxide gel, aluminum oxide; With various clays, as Attapulgus clay (aqueous neusilin), Poroceel clay (hydrated aluminum oxide).Preferred sorbent material is a gac.
In general, gac is the microcrystal of the non-graphitized form of carbon, has formed internal void after it is processed, just because of this, it has very big surface-area.Have been found that the surface-area (N of specially suitable gac
2, the BET method) and be 500-1500m
2/ g, preferred 900-1400m
2/ g, the Hg pore volume is 0.1-1.0ml/g, preferred 0.2-0.8ml/g.The pore volume that term " Hg pore volume " expression is measured with mercury porosimetry.Can access extraordinary result with the gac that also has following character: micro-pore diameter is distributed as 0.2-2nm, average out to 0.5-1nm, pore size distribution (mercury porosimetry) is 1-10000nm, preferred 1-5000nm, the total pore volume of measuring with nitrogen porosity method is 0.4-1.5ml/g, preferred 0.5-1.3ml/g.Other preferred physical features comprises: apparent bulk density is 0.25-0.55g/ml, and granularity is 0.4-3.5nm, preferred 0.5-1.5nm, and whole crushing strength is at least 0.8MPa, preferably is at least 1.0MPa.The example of the suitable gac that can be purchased comprises Chemviron F-400 (FILTRASORB 400), DARCO GCL 8*30 and the DARCO GCL 12*40 (FILTRASORB and DARCO are trade marks) of Chemviron type.
The gac of Shi Yonging dry activated carbon preferably in the method for the invention.This expression is in the gross weight of gac, and the water-content of gac should preferably less than 1wt%, be more preferably less than 0.5wt% less than 2wt%.This often means that gac must carry out drying earlier before being used for method of the present invention.Can be with traditional drying method known in the art outside the venue or carry out drying at the scene.The example of suitable desiccating method be in nitrogen atmosphere in 100-500 ℃ temperature range with dry 1-48 hour of gac.Under the situation of using activated carbon and fixed bed, preferred field drying gac is about to carry out drying after the gac filling becomes bed.
In order further to improve the quality of base oil, the contact conditions of bottom product and gac (temperature, pressure, air speed) can change in very wide scope.Have been found that: suitable in this respect temperature range is 20-300 ℃, preferred 30-200 ℃, and more preferably 40-150 ℃.The working pressure of method of the present invention is not crucial especially, can be 1-200bar, preferred 1-100bar, most preferably 1-20bar.Have been found that: the little hourly space velocity of suitable weight is 0.2-25kg/l/hr, preferred 0.5-10kg/l/hr, more preferably 1-5kg/l/hr.Method of the present invention is suitable for carrying out under the condition that does not add hydrogen.
Can obtain the medicinal white oils of high yield with following method.A kind of method of utilizing following steps to prepare medicinal white oils or industrial white oil:
(a) will be from the raw material hydrocracking/hydroisomerization of Fischer-Tropsch process, wherein in raw material from Fischer-Tropsch process, having the compound of 60 or more a plurality of carbon atoms at least is 0.2 with having the weight ratio of the compound of 30 carbon atoms at least at least, and in the raw material from Fischer-Tropsch process, the compound of 30wt% has at least 30 carbon atoms at least;
(b) product separation of step (a) is become the base oil precursor fraction of one or more lower boiling cuts and wide region;
(c) base oil precursor fraction of the wide region that obtains in the step (b) is carried out the depression of pour point step;
(d) go out the heavy tower bottom distillate by product fractionation by distillation with step (c); With
(e) described tower bottom distillate is contacted with heterogeneous sorbent material.
Use in the step (a) from Fischer-Tropsch process than in the heavy feed stock, have at least the compound of 30 carbon atoms to account for 30wt% at least, preferably account for 50wt% at least, more preferably account for 55wt% at least.In addition, in the raw material from Fischer-Tropsch process, having the compound of 60 or more a plurality of carbon atoms at least is 0.2 with having the weight ratio of the compound of 30 carbon atoms at least at least, preferably is 0.4 at least, more preferably is 0.55 at least.Raw material from Fischer-Tropsch process preferably comes from fischer-tropsch products, C in this product
20The ASF-α value of+cut (the Anderson-Schulz-Flory chainpropagation factor) is 0.925 at least, preferably is 0.935 at least, more preferably is 0.945 at least, even more preferably is 0.955 at least.
Initial boiling point from the raw material of Fischer-Tropsch process reaches as high as 400 ℃, but preferably is lower than 200 ℃.Preferably, fischer-tropsch synthesis product is used as raw material from Fischer-Tropsch process in step (a) before, from fischer-tropsch synthesis product, have 4 or still less the compound and the compound separation of boiling point in this scope of carbon atom are gone out to the major general.Detailed earlier herein constitute the major part of fischer-tropsch synthesis product from the raw material of Fischer-Tropsch process, this raw material is through the hydrocracking step of the present invention's definition.Except that fischer-tropsch products, other cut also can become the part of raw materials from Fischer-Tropsch process.Other possible cut is suitably any high boiling fraction that obtains in the step (b).
This raw material from Fischer-Tropsch process is suitable for obtaining with Fischer-Tropsch process, and Fischer-Tropsch process can produce the fischer-tropsch products than heavy.Not all Fischer-Tropsch process can both produce such heavy product.The example of suitable Fischer-Tropsch process is described among WO-A-9934917 and the AU-A-698392.These methods can produce above-mentioned fischer-tropsch products.
Raw material and resulting wax residual solution product from Fischer-Tropsch process do not contain or contain considerably less sulfur-bearing and nitrogen compound.This is normal for the product that obtains by the Fischer-Tropsch reaction of using synthetic gas free from foreign meter substantially.The content of sulphur and nitrogen will be lower than detection limits usually, and the detection limits of sulphur is 5ppm at present, and nitrogen is 1ppm.
In order to remove the oxide compound that exists in the Fischer-Tropsch reaction product,, can choose the hydrotreating step that makes fischer-tropsch products stand appropriateness wantonly in order to make the olefin(e) compound that exists in the Fischer-Tropsch reaction product saturated.This hydroprocessing process is described among the EP-B-668342.The transformation efficiency that the appropriateness hydrotreating step preferably is expressed as in this step is lower than 20wt%, more preferably less than 10wt%.The application is defined as reaction with transformation efficiency and generates the weight percentage that boiling point that boiling point is lower than 370 ℃ of cuts is higher than 370 ℃ raw material.Through after so appropriate hydrotreatment, preferably from effluent, will have 3 or still less low-boiling compound and boiling point other compound in this scope of carbon atom remove, and then be used in the step (a).
Hydrocracking/the hygrogenating isomerization reaction of step (a) preferably carries out in the presence of hydrogen and catalyzer, and described catalyzer can be selected from those catalyzer that are applicable to this reaction known to a person of ordinary skill in the art.The catalyzer that is applicable to step (a) generally comprises acidic functionality and hydrogenation/dehydrogenation functional group.Preferred acidic functionality is a refractory metal oxide carriers.The suitable carriers material comprises silicon-dioxide, aluminum oxide, silica-alumina, zirconium white, titanium oxide and composition thereof.Be applicable to the solid support material that comprises in the catalyzer of the inventive method preferably carbonic acid gas, aluminum oxide and silica-alumina.Particularly preferred catalyzer comprises the platinum that loads on the silica-alumina carriers.If desired, by application halogen part, particularly fluorine on carrier, or use the acidity that the phosphorus part can improve support of the catalyst.Suitable hydrocracking/the hydroisomerization process and the example of appropriate catalyst are described among the EP-A-776959 of WO-A-0014179, EP-A-532118 and previous reference.
Preferred hydrogenation/dehydrogenation functional group is a VIII family metal, as nickel, cobalt, iron, palladium and platinum.The precious metal palladium of preferred VIII family, more preferably platinum.Catalyzer can comprise preferred noble metal hydrogenation/dehydrogenation active component, and in per 100 parts by weight, the amount of described active ingredient is the 0.005-5 weight part, preferred 0.02-2 weight part.The particularly preferred catalyzer that is used in hydroconversion stage comprises platinum, and in per 100 parts by weight, the amount of platinum is the 0.05-2 weight part, more preferably the 0.1-1 weight part.Catalyzer can also comprise binding agent, to improve catalyst strength.Binding agent can be non-acid, and its example is the known clay of those of ordinary skills and other binding agent.
In step (a), raw material is contacting in the presence of catalyzer under the High Temperature High Pressure with hydrogen.Temperature generally is 175-380 ℃, preferably is higher than 250 ℃, is more preferably 300-370 ℃.Pressure generally is 10-250bar, preferred 20-80bar.The little hourly space velocity of hydrogen gas supplied is 100-10000Nl/l/hr, preferred 500-5000Nl/l/hr.The little hourly space velocity of weight that hydrocarbon feed is supplied with is 0.1-5kg/l/hr, preferably is higher than 0.5kg/l/hr, more preferably less than 2kg/l/hr.Hydrogen can be 100-5000Nl/kg with the ratio of hydrocarbon feed, preferred 250-2500Nl/kg.
Being defined as the transformation efficiency that one way reaction generates in the step (a) of weight percentage of raw material that boiling point that boiling point is lower than 370 ℃ of cuts is higher than 370 ℃ is 20wt% at least, preferably is 25wt% at least, but preferably is not higher than 80wt%, more preferably no higher than 65wt%.The raw material that uses in the above-mentioned definition is the total hydrocarbon feed that adds step (a), therefore can also choose the more high boiling cut recirculation that will obtain in the step (b) wantonly.
In step (b), preferably the product separation with step (a) becomes the preferably base oil precursor fraction between 300-450 ℃ of one or more cuts, T10wt% boiling point.Can from the product of step (a), isolate heavy ends, to regulate the viscosity of resulting medical or industrial white oil.If do not remove heavy ends, then the kinematic viscosity of white oil in the time of 100 ℃ may be much larger than 15cSt.By regulating amount and the cut point that from the effluent of step (a), separates described heavy ends, can so that to the medical or industrial white oil kinematic viscosity 100 ℃ the time be 6cSt to greater than 25cSt.
If the separation of heavy cut, then the T90wt% boiling point of base oil precursor fraction is preferably between 350-550 ℃.Separate preferably by first distillation and carry out in that about atmospheric condition are following, preferred pressure is 1.2-2bara, wherein makes the higher product separation of gas oil product and low boiler cut such as petroleum naphtha and kerosene(oil)fraction and step (a) product.If from the product of step (a), remove high boiling fraction as above-mentioned, then thisly be suitable for 95wt% at least ebullient higher cut further separates in the vacuum distilling step under 370 ℃ the temperature being higher than, wherein obtain vacuum gas oil distillate, base oil precursor fraction and optional more high boiling fraction.Vacuum distilling is suitable for carrying out under the pressure of 0.001-0.05bara.
In step (c), the base oil precursor fraction that obtains in the step (b) is carried out depression of pour point handle.Depression of pour point should be interpreted as that all depressions of pour point that can make base oil more than 10 ℃, preferably reduce more than 20 ℃, more preferably reduce the technology more than 25 ℃.Described depression of pour point is handled and is preferably undertaken by so-called WITH CATALYTIC DEWAXING TECHNIQUE.
WITH CATALYTIC DEWAXING TECHNIQUE can be undertaken by any method that the regulation of front reduces by be present in the pour point that makes base oil precursor fraction at catalyzer and hydrogen.Suitable dewaxing catalyst is a heterogeneous catalyst, comprises molecular sieve, and chooses and have the metal such as the metallic combination of VIII family of hydrogenating function wantonly.Proved molecular sieve, preferably is the zeolite of intermediate pore size, has the good catalytic capability that reduces the base oil precursor fraction pour point under catalytic dewaxing condition.The bore dia of the zeolite of intermediate pore size is 0.35-0.8nm preferably.The zeolite of suitable intermediate pore size is mordenite, ZSM-5, ZSM-12, ZSM-22, ZSM-23, SSZ-32, ZSM-35 and ZSM-48.Another kind of preferred molecular sieve is silica-alumina phosphoric acid salt (SAPO) material, and SAPO-11 most preferably wherein is for example described in the US-A-4859311.Under situation about existing without any VIII family metal, ZSM-5 can choose wantonly with the form of its HZSM-5 and use.Other molecular sieve preferably uses with the VIII family metallic combination that adds.Suitable VIII family metal is nickel, cobalt, platinum and palladium.The example that may make up is Ni/ZSM-5, Pt/ZSM-23, Pd/ZSM-23, Pt/ZSM-48 and Pt/SAPO-11.Other details and the example of suitable molecular sieve and dewaxing condition for example are described among WO-A-9718278, US-A-5053373, US-A-5252527 and the US-A-4574043.
The also suitable binding agent that comprises of dewaxing catalyst.Described binding agent can be synthetic or natural (inorganic) material, as clay, silicon-dioxide and/or metal oxide.The example of natural clay is montmorillonite and kaolin families.Binding agent is the porous binder material preferably, refractory oxide for example, its example is: aluminum oxide, silica-alumina, silica-magnesia, silicon-dioxide-zirconium white, silica-thorium oxide, silica-beryllia, silicon-dioxide-titanium oxide, and ternary composition, as silica-alumina-Thorotrast, silica-alumina-zirconium white, silica-alumina-magnesium oxide and silica-magnesia-zirconium white.More preferably use the low acid refractory oxide binder material that does not have aluminum oxide basically.The example of these binder materials is two or more mixtures of silicon-dioxide, zirconium white, titanium dioxide, germanium dioxide, boron oxide and these examples of enumerating previously.Most preferred binding agent is a silicon-dioxide.
A preferred class dewaxing catalyst comprises above-mentioned intermediate zeolite crystallites and the above-mentioned low acid refractory oxide binder material that does not have aluminum oxide basically, and wherein the surface of aluminosilicate zeolite crystallites is by making aluminosilicate zeolite crystallites obtain modification through surperficial dealumination treatment.Preferred dealumination treatment is that the extrudate of binding agent and zeolite is contacted with the silicofluoride aqueous solution, for example described in US-A-5157191 or the WO-A-0029511.The example of above-mentioned suitable dewaxing catalyst is the Pt/ZSM-22 of Pt/ZSM-12, silica bound and dealuminzation of Pt/ZSM-23, silica bound and dealuminzation of Pt/ZSM-5, silica bound and the dealuminzation of silica bound and dealuminzation, for example described in WO-A-0029511 and the EP-B-832171.
Catalytic dewaxing condition is known in this area, generally comprise: service temperature is 200-500 ℃, be suitably 250-400 ℃, hydrogen pressure is 10-200bar, preferred 40-70bar, the little hourly space velocity of weight (WHSV) are every liter of catalyzer of 0.1-10kg oil per hour (kg/l/hr), are suitably 0.2-5kg/l/hr, be preferably 0.5-3kg/l/hr, hydrogen is that every liter of oily 100-2000 rises hydrogen with the ratio of oil.In the dewaxing step by between the 40-70bar between 315-375 ℃ transformation temperature, can prepare to have and be suitable at-10 ℃ of base oils to the different pour point specifications of-60 ℃ of variations.
In step (d), the dewaxing effluent of step (d) is chosen wantonly and be separated into one or more low viscosity base oil product and heavy base product product after being flashed out some low-boiling compounds.As mentioned above, this bottom product contacts with heterogeneous sorbent material in step (e).For example this tower bottom distillate can reach the specification of industrial white oil.Therefore, the invention still further relates to a kind of method that upgrades to medicinal white oils from the industrial white oil of Fischer-Tropsch process that makes, this method is with aforesaid way industrial white oil to be contacted with heterogeneous sorbent material.
The invention still further relates to a kind of medicinal white oils, its kinematic viscosity in the time of 100 ℃ is greater than 8.5cSt, non-annularity isoparaffin content is 80-98wt%, Saybolt color is+30, adsorb spectral value less than 0.70 according to the ultraviolet ray in the 280-289nm spectrum band that FDA 178.3620 (`c) measures by ASTM D 2269, ultraviolet ray absorption spectral value in the 290-299nm spectrum band is less than 0.60, ultraviolet ray in 300-329nm spectrum band absorption spectral value less than 0.40 and ultraviolet ray absorption spectral value in the 330-380nm spectrum band less than 0.09.
Above-mentioned medicinal white oils can be as softening agent or releasing process oil.This releasing agent can be advantageously utilised in the food product pack field.
With indefiniteness embodiment the present invention is described below.
Embodiment 1
Tower bottom distillate has the performance (raw material 1) that table 1 is enumerated, and this tower bottom distillate is by the raw material from Fischer-Tropsch process being carried out above-mentioned steps (a)-(d) obtain, preparing medicinal white oils with this cut.The raw material from Fischer-Tropsch process that uses in the step (a) is the C of fischer-tropsch products
5-C
750℃
+The product that uses the catalyzer of EXAMPLE III to obtain in example VII A in the cut, this fischer-tropsch products and WO-A-9934917 is identical.Described raw material contains the C of the 60wt% that has an appointment
30+ product.C
60+/C
30+ ratio be about 0.55.
Table 1
| Raw material 1 | Raw material 2 | |
| Kinematic viscosity in the time of 100 ℃ | 7.532 | ?11.11 |
| Density (d20/4) | 824.5 | ?831.2 |
| The 5wt% boiling point, Pt ℃ | 470 | ?479 |
| Pour point, ℃ | -9 | ?-45 |
| Saybolt color (ASTM D 156) | -4 | |
| ASlM color (ASTM D 1500) | ?L3.0 |
Make tower bottom distillate pass through " Chemviron " charcoal type F-400 dry raw grain bed about 100 hours with upflow mode down at 85 ℃ with the flow of 1g/g.h (about 0.41/l.h).
UV adsorptive value and Saybolt color are listed in the table 2.Result in the table 2 shows: be used for can obtaining medicinal white oils from the tower bottom distillate of Fischer-Tropsch process.In this embodiment, described tower bottom distillate has reached the specification of industrial white oil basically.Therefore, this embodiment has also proved with this simple absorption method and the industrial white oil from Fischer-Tropsch process can have been changed into medicinal white oils.
Embodiment 2
Repeat embodiment 1, difference is to use raw material 2.With obtaining raw material 2 with raw material 1 corresponding mode.Under higher temperature, carry out catalytic dewaxing, thereby obtain lower pour point for bottom fraction feed 2.
Table 2
| Performance-cut: | UV scope 280-289nm | ?290-29 ?9 ?nm | ?300-32 ?9 ?nm | ?330-38 ?0 ?nm | Saybolt color |
| Industrial white oil specification * (maximum value) | ?4 | ?3.3 | ?2.3 | ?0.8 | ＞+20 |
| Medicinal white oils specification * * (maximum value) | ?0.70 | ?0.60 | ?0.40 | ?0.09 | +30 |
| Raw material 1 | ?1.11 | ?1.65 | ?2.89 | ?0.9 | -4 |
| Raw material 2 | ?5.0 | ?4.6 | ?5.0 | ?5.4 | The color is too dark can not measure with Saybolt |
| The oil that embodiment 1 obtains | ?0.14 | ?0.10 | ?0.03 | ?0.01 | +30 |
| The oil that embodiment 2 obtains | ?0.12 | ?0.10 | ?0.06 | ?0.02 | +25 |
* measure with ASTM 2269 according to FDA 178.3620 (b)
* measures with ASTM 2269 according to FDA 178.3620 (`c)
Claims (4)
1. one kind is used for from the paraffinic hydrocarbons base product product preparation medicinal white oils of Fischer-Tropsch process or the method for industrial white oil described bottom product being contacted with heterogeneous sorbent material.
2. the process of claim 1 wherein that described sorbent material is a gac.
3. medicinal white oils from Fischer-Tropsch process, its kinematic viscosity in the time of 100 ℃ is greater than 8.5cSt.
4. each method of claim 1-3, wherein said bottom product obtains by following step:
(a) will be from the raw material hydrocracking/hydroisomerization of Fischer-Tropsch process, wherein in raw material from Fischer-Tropsch process, compound with at least 60 or more a plurality of carbon atoms is 0.2 with the weight ratio with compound of at least 30 carbon atoms at least, and in the raw material from Fischer-Tropsch process, the compound of 30wt% has at least 30 carbon atoms at least;
(b) product separation of step (a) is become the base oil precursor fraction of one or more more lower boiling cuts and wide region;
(c) base oil precursor fraction of the wide region that obtains in the step (b) is carried out the depression of pour point step;
(d) go out the heavy tower bottom distillate by product fractionation by distillation with step (c); With
(e) described tower bottom distillate is contacted with heterogeneous sorbent material.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP02291563.1 | 2002-06-24 | ||
| EP02291563 | 2002-06-24 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1662632A true CN1662632A (en) | 2005-08-31 |
| CN100419048C CN100419048C (en) | 2008-09-17 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB038146940A Expired - Fee Related CN100419048C (en) | 2002-06-24 | 2003-05-07 | Process to prepare medicinal and technical white oils |
Country Status (10)
| Country | Link |
|---|---|
| US (1) | US20050258074A1 (en) |
| EP (1) | EP1516038B1 (en) |
| JP (1) | JP4344826B2 (en) |
| CN (1) | CN100419048C (en) |
| AT (1) | ATE335063T1 (en) |
| AU (1) | AU2003240612A1 (en) |
| DE (1) | DE60307274T2 (en) |
| ES (1) | ES2270038T3 (en) |
| WO (1) | WO2004000975A1 (en) |
| ZA (1) | ZA200409056B (en) |
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| US7402236B2 (en) * | 2004-07-22 | 2008-07-22 | Chevron Usa | Process to make white oil from waxy feed using highly selective and active wax hydroisomerization catalyst |
| JP5254009B2 (en) * | 2005-05-20 | 2013-08-07 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Compositions containing the use of Fischer-Tropsch derived white oil for food contact applications |
| JP2008540791A (en) * | 2005-05-20 | 2008-11-20 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ | Fischer-Tropsch derived white oil-containing polystyrene composition |
| US20090036546A1 (en) * | 2007-07-31 | 2009-02-05 | Chevron U.S.A. Inc. | Medicinal Oil Compositions, Preparations, and Applications Thereof |
| DE102007042548A1 (en) * | 2007-08-30 | 2009-03-05 | Riepe, Angelika | Liquid release agent |
| EP2075314A1 (en) | 2007-12-11 | 2009-07-01 | Shell Internationale Research Maatschappij B.V. | Grease formulations |
| CN101998986B (en) | 2007-12-20 | 2014-12-10 | 国际壳牌研究有限公司 | Fuel compositions |
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| WO2009080681A2 (en) * | 2007-12-20 | 2009-07-02 | Shell Internationale Research Maatschappij B.V. | Process to prepare a gas oil fraction and a residual base oil |
| KR100921062B1 (en) | 2008-05-21 | 2009-10-08 | 현대자동차주식회사 | Lift device of active hood system |
| JP6266606B2 (en) | 2012-06-21 | 2018-01-24 | シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイＳｈｅｌｌ Ｉｎｔｅｒｎａｔｉｏｎａｌｅ Ｒｅｓｅａｒｃｈ Ｍａａｔｓｃｈａｐｐｉｊ Ｂｅｓｌｏｔｅｎ Ｖｅｎｎｏｏｔｓｈａｐ | Lubricating oil composition comprising heavy Fischer-Tropsch derived and alkylated aromatic base oil |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB815264A (en) * | 1955-10-17 | 1959-06-24 | Forsch Patentverwertung Ges | The production of white oil from used oils |
| US4574043A (en) * | 1984-11-19 | 1986-03-04 | Mobil Oil Corporation | Catalytic process for manufacture of low pour lubricating oils |
| US4859311A (en) * | 1985-06-28 | 1989-08-22 | Chevron Research Company | Catalytic dewaxing process using a silicoaluminophosphate molecular sieve |
| US5157191A (en) * | 1986-01-03 | 1992-10-20 | Mobil Oil Corp. | Modified crystalline aluminosilicate zeolite catalyst and its use in the production of lubes of high viscosity index |
| US5252527A (en) * | 1988-03-23 | 1993-10-12 | Chevron Research And Technology Company | Zeolite SSZ-32 |
| US5053373A (en) * | 1988-03-23 | 1991-10-01 | Chevron Research Company | Zeolite SSZ-32 |
| US5082986A (en) * | 1989-02-17 | 1992-01-21 | Chevron Research Company | Process for producing lube oil from olefins by isomerization over a silicoaluminophosphate catalyst |
| JP3609830B2 (en) * | 1993-12-20 | 2005-01-12 | モービル・オイル・コーポレイション | Hydrogenation method |
| US6179994B1 (en) * | 1998-09-04 | 2001-01-30 | Exxon Research And Engineering Company | Isoparaffinic base stocks by dewaxing fischer-tropsch wax hydroisomerate over Pt/H-mordenite |
| US6332974B1 (en) * | 1998-09-11 | 2001-12-25 | Exxon Research And Engineering Co. | Wide-cut synthetic isoparaffinic lubricating oils |
| CN1075547C (en) * | 1998-09-28 | 2001-11-28 | 中国石油化工集团公司 | One-stage hydrogenation process for preparing industrial white oil |
| US6468417B1 (en) * | 1999-06-11 | 2002-10-22 | Chevron U.S.A. Inc. | Filtering lubricating oils to remove haze precursors |
-
2003
- 2003-05-07 CN CNB038146940A patent/CN100419048C/en not_active Expired - Fee Related
- 2003-05-07 WO PCT/EP2003/004853 patent/WO2004000975A1/en active IP Right Grant
- 2003-05-07 US US10/519,250 patent/US20050258074A1/en not_active Abandoned
- 2003-05-07 AT AT03729994T patent/ATE335063T1/en not_active IP Right Cessation
- 2003-05-07 JP JP2004514632A patent/JP4344826B2/en not_active Expired - Fee Related
- 2003-05-07 ES ES03729994T patent/ES2270038T3/en not_active Expired - Lifetime
- 2003-05-07 DE DE60307274T patent/DE60307274T2/en not_active Expired - Lifetime
- 2003-05-07 EP EP03729994A patent/EP1516038B1/en not_active Expired - Lifetime
- 2003-05-07 AU AU2003240612A patent/AU2003240612A1/en not_active Abandoned
-
2004
- 2004-11-09 ZA ZA200409056A patent/ZA200409056B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| ATE335063T1 (en) | 2006-08-15 |
| WO2004000975A1 (en) | 2003-12-31 |
| DE60307274T2 (en) | 2007-10-18 |
| EP1516038A1 (en) | 2005-03-23 |
| JP2005536578A (en) | 2005-12-02 |
| US20050258074A1 (en) | 2005-11-24 |
| ES2270038T3 (en) | 2007-04-01 |
| EP1516038B1 (en) | 2006-08-02 |
| ZA200409056B (en) | 2005-05-09 |
| CN100419048C (en) | 2008-09-17 |
| DE60307274D1 (en) | 2006-09-14 |
| AU2003240612A1 (en) | 2004-01-06 |
| JP4344826B2 (en) | 2009-10-14 |
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